Process and apparatus for 5 capturing gaseous ammonia

ABSTRACT

A method and system for collecting gaseous nitrogen compounds into an aqueous solution are provided. The method enables the combination of gaseous sulfur and nitrogen compounds in the aqueous solution to generate ammonium compound components, to include ammonium sulfate. Sulfur may be pressure injected into the solution as gaseous sulfur dioxide. Optionally, carbon may be introduced into the solution as gaseous carbon dioxide. The sulfur may be earlier sourced by a burning of a sulfurous solid. The pH of the solution may be monitored and the introduction of ammonia, carbon and/or sulfur may be halted or constrained while the pH of the solution is measured outside of specified range. The solution may be allowed to age to permit a mix of compounds of ammonium carbonate, ammonium bicarbonate and ammonium carbonate to restabilize and thereby encourage a renewed surge of ammonium sulfate generation.

CO-PENDING PATENT APPLICATION

This Nonprovisional Patent Application is a Continuation-in-PartApplication to Nonprovisional patent application Ser. No. 15/177,158filed on Jun. 8^(th), 2016 and titled “ PROCESS AND APPARATUS FORCAPTURING GASEOUS AMMONIA”. Nonprovisional patent application Ser. No.15/177,158 is hereby incorporated by reference in its entirety and forall purposes, to include claiming benefit of the priority date of filingof Nonprovisional patent application Ser. No. 15/177,158.

FIELD OF THE INVENTION

The present invention generally relates to the remediation of areas andmaterials that are present undesirable levels of nitrogen compounds,ammonia and/or ammonium compounds. More particularly, the presentinvention is directed to capturing gaseous ammonia in an aqueoussolution by precipitation and conversion into a non-volatile ammoniacalsalts.

BACKGROUND OF THE INVENTION

The subject matter discussed in the background section should not beassumed to be prior art merely as a result of its mention in thebackground section. Similarly, a problem mentioned in the backgroundsection or associated with the subject matter of the background sectionshould not be assumed to have been previously recognized in the priorart. The subject matter in the background section merely representsdifferent approaches, which in and of themselves may also be inventions.

Various natural processes, agricultural activities and sewage treatmentoperations generate outputs that include nitrogen compounds, ammoniumcompounds and ammonia, wherein the ammonia is generated in a gaseousstate and/or out-gasses at ambient temperatures. Factory farming oflivestock, offered as one example of a relevant industrializedagricultural activity that often generates excessive levels of nitrogencompounds and ammonia gas, is increasingly drawing attention as a sourceof nitrogen compounds pollution of soil, water and air. It is noted thatboth mammalian dung and avian feces contain nitrogen compounds that cancontribute to pollution of the natural environment. Sewage treatmentplants are also generally tasked with reducing or eliminating humancontribution to nitrogen compounds pollution of the environment. In anadditional area relevant to certain applications of the presentinvention, sites of drug and chemical manufacture can be contaminated byammonia gas and other compounds containing nitrogen.

The prior art provides methods of capturing ammonia by generatingconcentrated sulfuric acid solutions and transporting the concentratedacidic solution to a site where a target gaseous ammonia is located. Theconcentrated sulfuric acidic solution sulfuric is then mixed with awater volume to create an acid bath that is exposed to the targetammonia. This prior art method includes several short comings, not theleast of which are the costs of handling and transportation and the riskof metal contamination of the concentrated sulfuric acid solution duringstorage and transit.

Yet the prior art fails to provide optimal methods and systems thatenable the extraction of nitrogen from gaseous ammonia and ammoniumcompounds present in outputs of many widely practiced industrial andagricultural systems.

There is therefore a long-felt need to provide a method and apparatusthat enable the collection of nitrogen compounds from laboratoryfacilities, industrial sites and agricultural operations.

OBJECTS OF THE INVENTION

It is an object of the method of the present invention (hereinafter,“the invented method”) to remove gaseous ammonia from a site atmosphereby introducing sulfur dioxide as a solute to acidify an aqueoussolution, wherein the sulfur dioxide is generated by burning sulfuron-site, and whereby the resultant acidic aqueous solution absorbs thegaseous ammonia and generates resultant chemical compounds that capturenitrogen from nitrogen compounds.

It is an optional object of the invented to generate ammonium sulfate asa resultant compound of interaction sponsored within the acidic aqueoussolution as a result of absorption of ammonia by the aqueous solution,and optionally absorbing carbon dioxide, from the site atmosphere.

It is an additional optional object of the invented method to absorbammonia and optionally absorbing carbon dioxide in the acidic aqueoussolution, wherein the ammonia and the carbon dioxide is generated bybacterial processing of organic waste matter.

It is a still additional optional object of the invented to generateammonium sulfate as a resultant chemical compound of interaction of theacidic aqueous solution with ammonia, wherein the ammonia is generatedby bacterial processing of organic waste matter.

SUMMARY

Toward these and other objects that are made obvious in light of thepresent disclosure, an, organic ammonium sulfate product is produced byaerobically composting a source of nitrogen, such as animal waste ormanure mixed with a carbon source to create a biomass having a highsolids content, through highly selective aerobic bacteria action withoutaddition of external heat. Preferably, the production process includesthe steps of providing a composting apparatus located inside acomposting building such as a barn, a shed, or a greenhouse, housing acomposting trench; placing the animal waste or manure preferablycollected from a CAFOs facility in said composting trench; mixing saidanimal waste or manure with a source of carbon to form a biomass havinga high solids content; providing aerobic bacteria and supplying saidaerobic bacteria with water and oxygen in sufficient amounts to highlyselectively convert the waste amino acids, proteins, uric acid and anyother available nitrogen compounds from the biomass into NH₃ and/or NH₄and CO₂ without addition of external heat; moving said biomass down thecomposting trench as the aerobic composting process progresses;capturing the NH₃ and/or NH₄ and CO₂ from the atmosphere of thecomposting apparatus in an aqueous solution; adding a source of sulfateto said aqueous solution containing captured NH₃ and/or NH₄ and CO₂, andprocessing said aqueous solution containing a source of sulfate andcaptured NH₃ and/or NH₄ and CO₂ to obtain ammonium polycarbonate and/orsolid or concentrated liquid ammonium sulfate product. Preferably, theobtained ammonium sulfate product is certifiable as organic.

Certain alternate preferred embodiments of invented method and aninvented apparatus enable the extraction of nitrogen from gaseousammonia by the application of sulfur dioxide generated by burningsulfur. In an optional aspect of the invented method, gaseous ammonia isintroduced into an acidic aqueous solution and ammonium sulfate isproduced from the resulting aqueous solution. Sulfur and/or sulfurdioxide may be introduced into the aqueous solution to further acidifythe aqueous solution and sponsor the production of ammonium sulfate.Optionally of additionally, carbon and/or carbon dioxide may beintroduced into the aqueous solution to further sponsor the productionof ammonium sulfate.

In a first application of the invented method, a volume of source airthat comprises gaseous ammonia is introduced into an aqueous solutioncontaining sulfur dioxide. The source air containing the ammonia gas mayoptionally simply be introduced into the water volume without filteringout of any constituents and/or without any significant or intendedchemical processing.

In another optional aspect of the invented method, the internalatmosphere of an enclosed structure containing ammonia gas andoptionally carbon dioxide is at least partially scrubbed of the ammoniagas by exposing the enclosed internal atmosphere to an acidic aqueoussolution. The aqueous solution preferably comprises sulfur dioxidegenerated by burning sulfur in the presence of oxygen. The acidifiedaqueous solution having received the sulfur dioxide then is exposed togaseous ammonia to sponsor the production of chemical compounds withinthe aqueous solution whereby gaseous ammonia and nitrogen compounds areremoved from the internal atmosphere. Ammonium sulfate may be producedas a resultant compound in certain alternate preferred embodiments ofthe invented method.

In another optional aspect of the invented method, an enclosure isestablished at a site contaminated with a solid or liquid sourcematerial, wherein the source material contains ammonium compounds andemits gaseous ammonia. The enclosure may be a portable structure that istemporarily erected as the instant site and may be successivelyredeployed at alternate locations. Emission of ammonia gas may befacilitated or accelerated by aerating the source material, e.g.,mechanically tilling solid source material, or churning a liquid sourcematerial with ambient air containing oxygen. A resultant acceleration ofgaseous ammonia production by disturbance and/or introduction of oxygeninto the source material may be effected by the organic function ofbacteria present or seeded within the source material.

In yet another optional aspect of the invented method, the pH of theaqueous solution may be monitored and the introduction of ammonia,sulfur dioxide and/or carbon dioxide may be halted while the pH ismeasured outside of a prespecified range, e.g., a range of preferablyfrom approximately 4.0 to 5.0, or alternately a range of from 3.0 to6.0.

In a still additional optional aspect of the invented method, ammoniumsulfate is filtered out and/or extracted from the aqueous solution andoptionally provided for or used as an agricultural fertilizer. Theammonium sulfate may be removed from the aqueous solution as aconcentrated solution or in combination with a portion of the aqueoussolution.

In an even other optional aspect of the invented method, gaseous sulfurdioxide is pressure injected and/or infused into the aqueous solution tosponsor formation of solid ammonium sulfate, other precipitates, and/orchemical components.

In another optional aspect of the invented method, components areremoved from the aqueous solution and the resultant water is reused in afollowing cycle of scrubbing gaseous ammonia from an enclosed atmosphereand/or ammonium sulfate generation.

In a still other optional aspect of the invented method, the aqueoussolution may be allowed to age to permit a mix of compounds within theaqueous solution, including but not limited to ammonium carbonate,ammonium bicarbonate, ammonium carbonate and ammonium carbomate, torebalance and thereby sponsor a renewed surge of ammonium sulfategeneration.

This Summary and Objects of the Invention is provided to introduce aselection of concepts in a simplified form that are further describedbelow in the Detailed Description. This Summary is not intended toidentify key features or essential features of the claimed subjectmatter, nor is it intended to be used to limit the scope of the claimedsubject matter.

BRIEF DESCRIPTION OF THE DRAWINGS

These, and further features of the invention, may be better understoodwith reference to the accompanying specification and drawings depictingthe preferred embodiment, in which:

FIG. 1A is a process chart comprising aspects of the invented method;

FIG. 1B is a block diagram of a first preferred embodiment of theinvented apparatus (hereinafter, “first system”) coupled with a gaseousammonia source, the first system comprising a reaction chamber holding awater volume, an ammonia gas scrubber module coupled with the reactionchamber and the gaseous ammonia source, a sulfur dioxide module coupledwith the reaction chamber and providing sulfur dioxide to the watervolume, and a combined reverse osmosis module and electro dialysiscoupled with the reaction chamber;

FIG. 1C is a block diagram of a second preferred embodiment of theinvented apparatus (hereinafter, “second system”) coupled with a gaseousammonia source, the second system comprising the first system and anagitator module coupled with a source material, the agitator moduleadapted to encourage production of gaseous ammonia by the gaseousammonia source;

FIG. 1D is a block diagram a first preferred embodiment of the of theammonia gas scrubber module of FIG. 1B;

FIG. 1E is a block diagram of a first preferred embodiment of the sulfurdioxide module of FIG. 1B;

FIG. 1F is a block diagram a first preferred embodiment of the combinedreverse osmosis module and electro dialysis of FIG. 1B;

FIG. 2 is a flow chart of a first preferred embodiment of the inventedmethod (hereinafter, “first method”) that may be implemented by thefirst system of FIG. 1B and having optional aspects that may beimplemented by the second system of FIG. 1C;

FIG. 3 is a cut-away top view of the first system adapted todecontaminate an internal volume of air of a substantively enclosed andcontaminated structure, wherein the enclosed air includes gaseousammonia;

FIG. 4 is a cut-away side view of the first system adapted to remediatea liquid spill, wherein a portable tent source enclosure is placed aboveand around the liquid spill and an air pump is placed and positioned topump air into the liquid source material in order to sponsor anaccelerated production of source ammonia from the liquid spill bybacterial action;

FIG. 5 is an example of the first system enclosing an accumulation of asubstantively solid source material that emits ammonia gas, wherein thefirst system is augmented with a rototiller applied to agitate the solidsource material and accelerate the production and capturing of gaseousammonia;

FIG. 6 is a schematic diagram of an optional internal control system ofthe first system of FIG. 1A with optional modules that extend control tothe second system of FIG. 1B;

FIG. 7 is a schematic diagram of a controlled power distribution networkof the control system of the first system of FIG. 1A and includingoptional elements of the second system of FIG. 1B;

FIG. 8 is a cut-away view of elements of the first system of FIG. 1 thatdirect gaseous ammonia from the enclosure of the source material and todelivery within the reaction chamber;

FIG. 9 is a cut-away view of the distribution system for sulfur dioxidewithin the reaction chamber of the first system of FIG. 1;

FIG. 10 is a block diagram of a third alternate preferred embodiment ofthe present invention (hereinafter, “third system”) wherein a source ofpressurized carbon dioxide is provided and is adapted to deliver gaseouscarbon dioxide into the water volume and within the reaction chamber ofthe first system of FIG. 1;

FIG. 11 is a cut-away view of the distribution system for carbon dioxidewithin the reaction chamber of the third system of FIG. 11;

FIG. 12 is an illustration of a fifth motorized embodiment of the firstsystem of FIG. 1B;

FIG. 13 is an illustration of a carbon dioxide generation module thataccepts mammalian exhalation a source of gaseous carbon dioxide ascoupled with the third system of FIG. 10;

FIG. 14 is an alternate sixth preferred embodiment of the inventedmethod showing process outline comprising aspects of the inventedmethod;

FIG. 15 is a schematic diagram of equipment and structures comprising anoptional preferred setup of a production facility enabled forimplementation of the sixth preferred embodiment of the invented methodof FIG. 14;

FIG. 16 presents optional aspects and features of certain alternatepreferred embodiments of the invented composting apparatus, whereinammonia gas is produced by highly selective aerobic bacteria actionwithout requiring an addition of external heat energy beyond availableambient heat energy

FIG. 17 is a perspective view of a composting apparatus in accordancewith a seventh preferred embodiment of the present invention;

FIG. 18 is a perspective view of composting trench of compostingapparatus of FIG. 17; and

FIG. 19 is a flow chart of organic ammonium sulfate product manufactureprocess of a seventh preferred embodiment of the method of the presentinvention.

DETAILED DESCRIPTION OF THE INVENTION

It is to be understood that this invention is not limited to particularaspects of the present invention described, as such may, of course,vary. It is also to be understood that the terminology used herein isfor the purpose of describing particular aspects only, and is notintended to be limiting, since the scope of the present invention willbe limited only by the appended claims.

Methods recited herein may be carried out in any order of the recitedevents which is logically possible, as well as the recited order ofevents.

Where a range of values is provided herein, it is understood that eachintervening value, to the tenth of the unit of the lower limit unlessthe context clearly dictates otherwise, between the upper and lowerlimit of that range and any other stated or intervening value in thatstated range, is encompassed within the invention. The upper and lowerlimits of these smaller ranges may independently be included in thesmaller ranges and are also encompassed within the invention, subject toany specifically excluded limit in the stated range. Where the statedrange includes one or both of the limits ranges excluding either or bothof those included limits are also included in the invention.

Unless defined otherwise, all technical and scientific terms used hereinhave the same meaning as commonly understood by one of ordinary skill inthe art to which this invention belongs. Although any methods andmaterials similar or equivalent to those described herein can also beused in the practice or testing of the present invention, the methodsand materials are now described.

It must be noted that as used herein and in the appended claims, thesingular forms “a”, “an”, and “the” include plural referents unless thecontext clearly dictates otherwise. It is further noted that the claimsmay be drafted to exclude any optional element. As such, this statementis intended to serve as antecedent basis for use of such exclusiveterminology as “solely,” “only” and the like in connection with therecitation of claim elements, or use of a “negative” limitation.

It will be appreciated that terms such as “front,” “back,” “top,”“bottom,” “left,” “right,” “horizontally,” “up,” “down,” and “side” usedherein are merely for ease of description and refer to the orientationof the components as shown in the figures. It is to be understood thatany orientation of the apparatus, and the components thereof describedherein, is within the scope of the present invention.

In a preferred embodiment, the term “organic” as used herein is alabeling certification term that refers to an agriculture productproduced in accordance with the Code of Federal Regulations (“CFR”)Title 7 (Subtitle B, Chapter I, Subchapter M, Part 205). As usedhereinafter, “organic ammonium sulfate” is interchangeable with“ammonium sulfate,” “organic ammonium sulfate product,” and/or“product.” As used herein, “plurality” means “one or more.”

Referring now generally to the Figures and particularly to FIGS. 1A, 1Band 1C, FIG. 1A is a process chart comprising aspects of the inventedmethod that may be instantiated by the first preferred embodiment 100 ofthe present invention (hereinafter, “the first system 100”). In step1.00 the first system 100 is preferably co-located with a volume ofsource ammonia gas 102. In step 1.02 and proximate to a water volume104, a sulfur mass 106 in a solid form is burned in the presence ofatmospheric oxygen 108 to form gaseous sulfur dioxide 110. Thetemperature of the source ammonia gas 102 and the water volume 104 isinitially preferably within 5 degrees Celsius of the ambient temperatureof the site environment of the first system 100 and also preferablywithin the temperatures range of greater than the freezing point of thewater volume 104 and less than the boiling point of the water volume104.

The water volume 104 is then acidified in step 1.04 by introduction ofthe sulfur dioxide 110 to form an acidic aqueous solution 112, asindicated in FIG. 1C.

The acidic aqueous solution 112 is then exposed to the source ammoniagas 102, and optionally carbon dioxide, in step 1.06, wherein portionsof the source ammonia gas 102, and optionally gaseous carbon dioxide, isabsorbed by the aqueous solution 112 in step 1.06. It is understood thatthe source ammonia gas may 102 may be comprised within an enclosedatmospheric gas 114 that includes other atomic and molecular components,such as carbon dioxide, and that the acidic aqueous solution 112 mayabsorb carbon dioxide and additional molecules and free atoms from theenclosed atmospheric gas 114 in step 1.06. It is further understood thatthe enclosed atmospheric gas 114 may be formed by adding ammonia, carbondioxide and other products of bacteria acting on organic waste, e.g.,dung or feces, to a pre-existing ambient atmosphere.

Precipitates, other solutes and/or certain non-aqueous components of theaqueous solution 112, e.g., ammonium sulfate, are concentrated andcollected by circulation through a collection module 116 in step 1.08 toform an output solution 128 that is held in a holding tank 130 forremoval from the first system 100, and the pH of the aqueous solution112 is monitored in step 1.10. When a pH measurement of greater than 5.0is determined in step 1.12, the rate of volumetric exposure of thegaseous sulfur dioxide 110 is increased in step 1.14, and when a pHmeasurement of lower than 4.0 is determined in step 1.16, the rate ofvolumetric exposure of the gaseous sulfur dioxide 111 is decreased instep 1.80

It is understood that the aqueous solution 112 is preferablysubstantively and continuously exposed to gaseous sulfur dioxide 110 insteps 1.06 through 1.18 albeit possibly at varying rates of volumetricexposure to the sulfur dioxide gas 110 is increased in step 1.14. It isfurther understood that the absorption of the source ammonia gas 102indicated in step 1.06 and the collection of solutes and non-aqueouscomponents of the aqueous solution of step 1.08 are preferablycontinuously and contemporaneously occurring during the instantiation ofthe loop of steps 1.06-1.18.

An operator or an automated control system 118 may act and/or elect tostop the process loop of steps 1.02 through 1.18 in step 1.20 wherebythe burning of the sulfur mass 106 and the processes of steps 1.04through 1.18 are halted are minimized.

Referring now generally to the Figures and particularly to FIG. 1B, FIG.1B is a block diagram of the first system 100 that includes certainoptional elements. The first system 100 is coupled to a source enclosure120 that contains the source ammonia gas 102 and the enclosedatmospheric gas 114. The source ammonia gas 102 may be emitted from asource material 121 containing ammonium and/or ammonium compounds, andthe first system 100 is adapted to withdraw the source ammonia gas 102,by itself and/or mixed within the enclosed atmospheric gas 114 locatedwithin the source enclosure 120, into an ammonia scrubber module 122through which the water volume 104 is circulated. The water volume 104is maintained within a reaction chamber 124 and the ammonia scrubbermodule 122 (hereinafter, “the ammonia scrubber module 122”) is coupledto both the source enclosure 120 and the reaction chamber 124 and isfurther adapted to circulate the aqueous solution 112 to absorb thesource ammonia gas 102. The source ammonia gas 102 is thus removed fromthe source enclosure 120 and inserted into the water volume 104 as thewater volume 104 is circulated through the ammonia scrubber 122. Asulfur dioxide generation module 126 is also coupled with the reactionchamber 124 and is adapted to insert or infuse the gaseous sulfurdioxide 110 into the water volume 104 to form the aqueous solution 112as the water volume 104 is circulated through the sulfur dioxidegeneration module 126. The collection module 116 is a combined reverseosmosis module and electro dialysis module 116 (hereinafter, “the RO/EDmodule 116”) and is additionally coupled with the reaction chamber 124by tuning 144 to withdraw aqueous solution 112 and preferably returnwater volume 104. The RO/ED module 116 is adapted to remove certainchemicals, e.g., ammonium sulfate, from the aqueous solution 112 as theaqueous solution 112 is circulated through the RO/ED module 116. Aconcentrate output holding tank 126 is coupled with the RO/ED module 116and is adapted to receive a concentrated output solution 128 formedwithin the RO/ED module 116 and containing both (a.) a portion of thewater volume 104 as a solvent and (b.) a solute or component of at leastone type of resultant chemical, e.g., ammonium sulfate, formed withinthe aqueous solution 112 by the invented method. The aqueous solution112 and the concentrated output solution 128 may thus include ammoniumsulfate as a solute or component, whereby ammonium sulfate is producedin a manner that is in conformance one or more governmental, regulatoryor organizational standards and the resultant ammonium sulfate mayreceive a certification of a preferred or particular origin, such as abeing certified, graded, trademarked or marked as a special type oforganic sulfate. It is understood that the receipt of suchcertifications or authorizations may increase the market value andperceived quality of the resultant ammonium sulfate of the concentratedoutput solution 128.

It is also understood that the first system 100 may include commerciallyavailable equipment or their equivalents, wherein the ammonia scrubber122 may be or comprise, or be comprised within, a wet flue gas scrubbermarketed by Deryck A Gibson Ltd. of Kingston Jamaica. In variousalternate preferred embodiments of the present invention, the acidifiedaqueous solution 112 may presented to the source ammonia gas 102 withinthe ammonia scrubber 122 as a mist, a spray or a waterfall as theaqueous solution 112 is circulated through the ammonia scrubber 122. Thereaction chamber 124 may comprise sheets, walls, a bottom wall and or/ceiling wall of polyvinyl chloride or other suitable material known inthe art.

The sulfur dioxide module 126 may be or comprise, or be comprisedwithin, a sulfur dioxide burner system as marketed by Harmon SystemsInternational, LLC of Bakersfield, Calif., whereby the sulfur dioxidegas 110 may be generated and commingled with water volume 104 that iscirculated through the sulfur dioxide module 126. It is understood thatthe Harmon sulfur dioxide burner system oxidizes sulfur 106 into sulfurdioxide gas 110 by burning the elemental sulfur 106 with a propane torchin the presence of a pressurized circulating portion of the water volume104 and air containing oxygen 108. The sulfur dioxide gas 110 iscombined with the water volume 104 to produce sulfurous acid, or H2SO3,within the aqueous solution 112

In addition, the RO/ED module 116 may be or comprise, or be comprisedwithin, a reverse osmosis/electro dialysis system as marketed byAmeridia Corporation of Moerdjik, Netherlands.

A control module 200 of the first system 100 generates and communicatescommands to direct the activity, and provides electrical power thatenables the functioning, of the first system 100 in the removal gaseousammonia and the generation of resultant chemical compounds andprecipitates e.g., ammonium sulfate. A communications and power bus 132of the control module 118 enables the control module 118 to send andreceive commands and data within the first system 100 and selectivelyand controllably provide power to other modules 116 122, 126, supplyfans SF01, supply pumps SP01-SP04, motorized fluid return pumps R01-R03,and an output pump OP01.

Referring now generally to the Figures and particularly to FIG. 1C, FIG.1C is a block diagram of a second preferred embodiment of the inventedsystem 136 (hereinafter, “the second system 136”) that includes thefirst system 100 and an agitator module 138 having an effector 140. Theeffector 140 is positioned relative to the source material 121 and isadapted to agitate the source material 121 in order to sponsor bacterialactivity that accelerates a production of the source ammonia gas 102 forcapture within the enclosure. The agitator module 140 may be or comprise(a.) a motorized rototiller, wherein the effector 140 is or comprises amechanical arm or rake that is motor driven to mechanically disturb andaerate the source material 121; (b.) a pressurized air pump, wherein theeffector 140 is or comprises a gas hose that delivers pressurizedambient air into the source material 121 and thereby disturbs andaerates the source material 121 with the pressurized ambient air.

Referring now generally to the Figures and particularly to FIG. 1D, FIG.1D is a detailed block diagram of a first preferred embodiment of theammonia scrubber 122. A first fluid supply pump SP01 as energized by ascrubber system control module 142 and/or the control system 118 pumpsportions of the aqueous solution 112 from the reaction chamber 124through substantively chemically inert tubing 144 through one or moreaeration fixtures 146-150 to enable the aqueous solution 112 to absorbthe source ammonia 102. The ammonia scrubber 122 further comprises ascrubber interface 154 that is bidirectionally communicatively coupledwith the control module 118 via the communications and power bus 132.The scrubber interface 154 is additionally bi-directionallycommunicatively coupled with, or comprised within, the scrubber systemcontrol module 142.

The aqueous solution 112 passes through the source ammonia gas 112 andfalls by gravity into a scrubber tank 152. A first aeration fixture 146releases the aqueous solution 112 within the ammonia scrubber 122 as asheet of fluid. A second aeration fixture 148 is a showerhead thatreleases the aqueous solution 112 into the source ammonia gas 102 as afine water mist. A third aeration fixture 150 is a showerhead thatreleases the aqueous solution 112 into the source ammonia gas 102 aswater droplets.

A first motorized fluid return pump SP01 as energized by the scrubbersystem control module 142 and/or the control system 118 pumps theaqueous solution 112 captured by the scrubber tank 152 throughadditional tubing 144 and thereby returns the aqueous solution 112 tothe reaction chamber 124. An optional first supply fan SF01 as energizedby the scrubber system control module 142 and/or the control system 118propels or drives the source ammonia gas 102 and the enclosedatmospheric gas 114 from the enclosure 120 and into the ammonia scrubber122 through a length of tubing 144. The scrubber tank 152 may comprisesheets, walls, a bottom wall and/or ceiling wall of polyvinyl chlorideor other suitable material known in the art.

It is understood that the ammonia scrubber 122 may be or comprise asuitable and commercially available gas scrubber known in the art, andthat the source fan SF01, the first motorized fluid supply pump SP01and/or the first motorized fluid return pump RP01 may be comprisedwithin the ammonia scrubber 122. It is further understood that thetubing 144 may be or comprise polyvinyl chloride piping or othersuitable and preferably substantively chemically inert material known inthe art.

Referring now generally to the Figures and particularly to FIG. 1E, FIG.1E is a detailed block diagram of a first preferred embodiment of thesulfur dioxide module 126. A second motorized fluid supply pump SP02 asenergized by an SO2 module control module 156, and/or the control system118, and thereupon pumps and circulates portions of the aqueous solution112 from the reaction chamber 124 through substantively chemically inerttubing 144 through a pressure column module 158. The pressure columnmodule 158 creates a pressure differential that infuses and/orintroduces sulfur dioxide gas 110 into the water volume 104 to form andacidify the aqueous solution 112. An ignition chamber 160 is adapted tomaintain the sulfur 106 within the sulfur module 126 before and duringof the ignition of the sulfur 106. The ignition of the sulfur 106 may beaccomplished by a user manually applying a flame 161 to the sulfur 106or by an electronically controlled ignition device 161B that (a.) issuesa flame or an igniting spark to the sulfur 106 when energized, or (b.)receives an ignition command message from the SO2 module controller 156and/or the control system 118 and is thereby directed to generate aspark, a blue flame and/or another sulfur ignition medium known in theart. Still alternatively, optionally or additionally, the sulfur 106 maybe or comprise touch-to-burn sulfur and may be manually ignited.

An SO2 module interface 162 is disposed between, and bi-directionallycommunicatively coupled with both of, the control system 118 and the SO2module controller 156. Bi-directional communications between the controlmodule 200 and the SO2 module controller 156 are enabled by thecommunications and power bus 132 and the SO2 module interface 162,whereby commands and data may be communicated to and from the controlmodule 200 and the SO2 module controller 156. Electrical power is alsoprovided to the sulfur dioxide module 126 via the communications andpower bus 132 and the SO2 module interface 162.

Optionally and alternatively electrical power and/or commands areprovided electronically controlled ignition device 161B by acommunicative coupling of the electronically controlled ignition device161B with the SO2 module controller 156 and/or the power andcommunications bus 132 of the control system 118.

It is understood that the sulfur module 126 may be or comprise a sulfurburner as marketed by Harmon Systems International, LLC of Bakersfield,Calif., or other suitable sulfur burner known in the art. It is furtherunderstood that the sulfur burner 126 may be or comprise a suitable andcommercially available sulfur burner known in the art, and that thesecond motorized fluid supply pump SP02 and/or the second motorizedfluid return pump RP02 may be comprised within the sulfur burner 126.

FIG. 1F is a block diagram of a first preferred embodiment of the RO/EDmodule 116. The RO/ED module 116 may include a reverse osmosis module164, an electro-dialysis module 166, a reverse osmosis electro dialysiselectronic logic controller module 168 (hereinafter, “RO/ED controller168”), an electronic interface 170 to the reverse osmosis electrodialysis electronic logic controller module (hereinafter, “RO/EDinterface 170”) and a second motorized fluid output pump OP02. It isunderstood that one or more of the third motorized fluid supply pumpSP03, the third motorized fluid return pump RP03, the fourth motorizedfluid return pump RP04, the first motorized fluid output pump OP01, andthe output holding tank 130 may be optionally or additionally comprisedwithin the RO/ED module 116. Bi-directional communications between thecontrol module 200 and the RO/ED controller 168 is enabled by thecommunications and power bus 132 and the RO/ED interface 170, wherebycommands and data may be communicated to and from the control module 200and to the RO/ED controller 168. Electrical power is also provided tothe RO/ED module 116 via the communications and power bus 132 and theRO/ED interface 170.

The RO/ED controller 168 is optionally bidirectionally communicativelycoupled to the reverse osmosis module 164 and may provide requiredelectrical power and control signals to the reverse osmosis module 164that direct and enable the reverse osmosis module 164 to substantivelyextract water volume from the aqueous solution 122 by reverse osmosis.The RO/ED controller 168 is further optionally bidirectionallycommunicatively coupled to the electro-dialysis module 166 and mayprovide required electrical power and control signals to theelectro-dialysis module 166 that direct and enable the electro-dialysismodule 166 to substantively extract additional water volume from theaqueous solution 122 by electro dialysis. The aqueous solution 112 isdelivered to the reverse osmosis module 164 by energizing the thirdmotorized fluid supply pump SP03 via a length of tubing 144. After somewater volume 104 is extracted from the aqueous solution 112 by thereverse osmosis module 164, the resultant aqueous solution 112 isdelivered to the electro dialysis module 166 from the reverse osmosismodule 164 by energizing the second motorized fluid output pump OP02.The RO/ED controller 168 is additionally optionally electrically coupledto the second motorized fluid output fluid pump OP02 and selectivelyprovides electrical power to energize the second motorized fluid outputfluid pump OP02 to enable transfer of the aqueous solution 112 from thereverse osmosis module 164 and to the electro dialysis module 166.

The RO/ED controller 168 and/or the control module 200 may optionally oradditionally be coupled to the third motorized fluid supply pump SP03and/or the third motorized fluid return pump RP03 and selectivelyenergize the third motorized fluid supply pump SP03 and/or the thirdmotorized fluid return pump RP03 to enable a delivery of the aqueoussolution 112 to the reverse osmosis module 164 and return of watervolume 104 from the reverse osmosis module 164 to the reaction chamber124. The RO/ED controller 168 and/or the control system 118 may furtheroptionally or additionally be coupled to the fourth motorized fluidreturn pump RP04 and selectively energize the fourth motorized fluidreturn pump RP04 to enable a return of water volume 104 from the electrodialysis module 166 to the reaction chamber 124. The RO/ED controller168 and/or the control system 118 may further optionally or additionallybe coupled to the first motorized fluid output pump OP01 and selectivelyenergize the first motorized fluid output pump OP01 to enable transferof the output solution 128 from the electro dialysis module 166 to theholding tank 130. The holding tank 130 may be or comprise one or morewalls, floor wall, and/or ceiling comprising polyvinyl chloride or othersuitable material known in the art.

An optional or additional RO/ED tubing length 172 may couple the reverseosmosis module 164 and the fourth motorized fluid return fluid pump RP04and may enable the fourth motorized fluid return fluid pump RP04 todrive water volume from both the reverse osmosis module 164 and theelectro dialysis module 166 and into the reaction chamber 124. The RO/EDtubing length 172 may be or comprise perforated polyvinyl chloridepiping and/or other suitable and substantively chemically inert materialknown in the art.

Referring now generally to the Figures and particularly to FIG. 2, FIG.6 and FIG. 7, FIG. 2 is a software flow chart implemented by of thecontrol system 118. In step 2.02 a command is sent from a control module200 of the control system 118 to the sulfur dioxide module 126 to ignitethe sulfur 106. In optional step 203 the control module 200 directs, andelectrically powers, the agitator module 138 to agitate the sourcematerial 121 and to thereby sponsor bacterial activity that willgenerate gaseous ammonia 102 and optionally carbon dioxide within theenclosure 120. The volume of gaseous ammonia preferably includesmolecules of NH3 and molecules of NH4+.

In step 2.02 another command is sent from the control module 200 in step2.04 to (a.) energize motorized fluid pumps SP02 & RP02 to circulatewater volume 104 and (b.) inject the resultant sulfur dioxide gas 110via the pressure column 158 into the water volume 104 to generate theaqueous solution 112. In step 2.06 the control module 200 accepts pHsensors SPh.01-SPh.N positioned within or proximate to the reactionchamber 124 to determine the pH of aqueous solution 112, and when the pHof the aqueous solution is not sensed to be greater than 4.0, thecontrol system 118 directs the sulfur dioxide module 126 to simplycontinue inject sulfur dioxide 110 into the aqueous solution 112 untilthe aqueous solution 112 is measured by the pH sensors SPh.01-SPh.N tohave exceeded a magnitude of approximately 4.0.

When the control module 200 receives a pH reading in step 2.06 greaterthan 4.0 from the pH sensors SPh.01-SPh.N, the control module 600proceeds on to step 2.08 and energizes the ammonia scrubber 122 in step2.08, whereby the ammonia scrubber 122 circulates the aqueous solution112 through the ammonia scrubber 112 and exposes the aqueous solution112 to the source ammonia gas 112. In optional step 2.09 the controlsystem 118 directs an optional carbon dioxide module 202, as furtherdisclosed in reference to FIG. 11, to initiate delivery of carbondioxide into the aqueous solution 112 within the reaction chamber 124.

The control module 600 directs the RO/ED module 116 in step 2.10 tocirculate the aqueous solution 112 through the RO/ED module 116 and togenerate an output solution 128 for storage in the output holding tank130.

In step 2.12 the control module 600 determines whether to continue theprocess of step 2.04 through 2.10, whereby portions of the aqueoussolution are substantively continuously and contemporaneously circulatedto and from the reaction chamber 124 and (a.) the sulfur dioxide module126 to receive sulfur dioxide; (b.) the ammonia scrubber 122 to absorbsource ammonia gas 102; and (c.) the RO/ED module 116 to filter outcomponents, e.g., ammonium sulfate; and to generate the output solution128. It is understood that the output solution contains (a.) a portionof the water volume 104 and (b.) one or more non-aqueous components ofthe aqueous solution 112 that have been separated from the aqueoussolution 112 by the RO/ED module 116. The control module 200 might, forexample, be programmed to proceed to step 2.13 and to shut down thefirst system 100 or the second system 136 when an ammonia gas detectorSA01 sends a measurement that indicates that that the concentration ofthe source ammonia gas 102 within the atmospheric gas 114 within theenclosure 120 is less than a pre-specified amount, e.g., less than oneparts per million per volume unit.

In the alternative, in step 2.12 a human operator may direct the controlsystem via an input module 202 to cease operations and proceed to step213 and to shut down the first system 100 or the second system 200.

The control system 118, in accordance with its structure, inputs andprogramming, may proceed from step 2.12 and to execute the loop of steps2.14 through 2.28, whereby the control system 118 directs the firstsystem 100 or the second system 136 to maintain a pH of the aqueoussolution 112 approximately within a preferred range, such asapproximately within the range of from 4.0 to 5.0 plus or minus five percent.

When the control module 200 determines in step 2.14 that the pH of theaqueous solution 112 is measured to be greater than 5.0, the controlsystem 118 proceeds on to step 2.16 and pause the activity of theammonia scrubber 122 in circulating and exposing aqueous solution 112for absorption of ammonia gas 102 and in step 2.18 directs the sulfurdioxide module 126 to increase the rate of introduction of sulfurdioxide 110 into the aqueous solution 110. An optional wait step 2.20imposes a wait state of a predetermined time, and in step 2.22 thecontrol system 118 directs the ammonia scrubber 122 to resumecirculating aqueous solution 112 and causing absorption of the sourceammonia gas 102 into the aqueous. The control system 118 directs thesulfur dioxide module 126 to resume a preprogrammed or pre-specifiedstandard rate of introduction of sulfur dioxide 110 into the aqueoussolution.

In the alternative, when the control module 200 determines in step 2.14that the pH of the aqueous solution 112 is not measured to be greaterthan 5.0, the control system 118 proceeds on to step 2.26 and todetermine if that the pH of the aqueous solution 112 is measured to beless than 4.0. When the control system 118 to determines in step 2.26that the pH of the aqueous solution 112 is measured to be less than 4.0,the control system 118 directs the sulfur dioxide module 126 to decreasethe rate of introduction of sulfur dioxide 110 into the aqueous solution110 to a certain pre-specified or preprogrammed rate of introduction ofsulfur dioxide 110 into the aqueous solution 110. The control module 200proceeds from either step 2.26 or step 2.28 to step 2.12.

It is understood that alternative control methods to implement theinvented method are made obvious to one of ordinary skill in the art inlight of the present invention. In certain alternate preferred methodsof the present invention, manual control, material input and/or materialoutput may be applied, effected or enabled by a human operator toengage, disengage, turn on and/or turn-off one or more modules 116, 122& 126, the source fan SF01, one or more motorized fluid pumps OP01,OP02, SP01-SP03 & RP01-RP04.

FIG. 3 is a cut-away top view of the first system 100 adapted todecontaminate the internal volume of air 300 of a substantively enclosedand contaminated structure 302, wherein the enclosed volume of air 300includes the source gaseous ammonia 102.

FIG. 4 is a cut-away side view of the first system 100 adapted toremediate an ammonia gas emitting and substantively liquid material 400,wherein a portable tent source enclosure 402 is placed above and aroundthe substantively liquid material 400 and an optional motorized air pump404 is placed and positioned to pump air into the liquid spill material400 through a tubing 406 in order to sponsor an accelerated productionof source ammonia 102 from the substantively liquid material 400 bybacterial action. An air pump controller 408 is electrically coupledwith both the motorized air pump motor 404 and the power andcommunications bus 132, whereby the air pump controller 408 receiveselectrical power to energize the air pump 404 via the power andcommunications bus 132, wherein the control system 118 selectively andcontrollably delivers electrical power to the air pump controller 408.

FIG. 5 is an example of the first system 100 enclosing an accumulationof a substantively solid collection of bird excrement or animal dung 500(hereinafter, “dung 500”) housed within an enclosure 502. The dung 500emits the source ammonia gas 102. The first system 100 is augmented witha tilling blade 504 that is rotatably coupled with an agitator motor506. The tilling blade 504 is adapted and applied to mechanically turnover and agitate the dung 500 and thereby accelerate the production andcapturing of the gaseous ammonia 102. The

An agitator motor controller 508 is electrically coupled with both theagitator motor 506 and the power and communications bus 132 and receiveselectrical power to energize the agitator motor 506 via the power andcommunications bus 132, wherein the control system 118 selectively andcontrollably delivers electrical power to the agitator motor 506.Additionally, alternatively or optionally, the agitator motor 506, thetilling blade 504 and the agitator motor controller 508 may be or becomprised within an automated COMPOST-A-MATIC (TM) in-vessel compostingsystem as marketed by Farmer Automatic of America, Inc. of Register, Ga.or other suitable motorized or automated tilling system known in theart. It is understood that the agitator module 138 may optionally oralternatively be or comprise an isolated stand-alone system that is notcoupled with the power and communications bus 132 and receives anindependent feed of electrical power.

FIG. 6 is a schematic diagram of an optional internal control system 118of the first system 100 with optional modules that extend control to thesecond system 136. The control module 200 includes a real time clock 600coupled with a logic controller 602. The logic controller 602 may becoupled with an optional memory 604. The logic controller 602 may be aprogrammable logic unit that directs the first system 100 to perform theinvented method, to include the aspects of the method of FIG. 2, and/orthe logic control 602 might be configured or adapted to executeprogramming of a software program stored within the memory 604. Thecontrol module 200 is bi-directionally communicatively coupled by meansof a communication bus 606 with the ammonia scrubber interface 154, thesulfur dioxide module interface 162, the RO/ED module 116, one or morepH sensors SpH.01-Sph.N and one or more ammonia gas concentrationsensors SA.01-SA.N. The communication bus 606 is preferably comprisedwithin the power and communications bus 132.

The control module 200 may optionally or additionally be coupled withthe agitator motor controller 504 and/or the agitator pump controller406. The control module 200 may be further optionally or additionally becoupled with a carbon dioxide valve controller 608 of the carbon dioxidesource module 202 of the second system 136, and as further disclosed inreference to FIGS. 6, 7 and 11.

FIG. 7 is a schematic diagram of a controlled power distribution network700 of the control system 118 of the first system 100 of FIG. 1A andincluding optional elements of the second system 136. The powerdistribution network 700 selectively and as controlled by the controlmodule 200 delivers electric power from an electrical power source 702to the ammonia scrubber 122, the sulfur dioxide module 126, the RO/EDmodule 116, one or more pH sensors, one or more ammonia gasconcentration sensors, one or more motorized fluid pumps OP01,SP01-SP-04 & RP01-RP-03, and/or the source fan SF01 of the first system100. Additionally or alternatively, power distribution network 700selectively and as controlled by the control module 200 deliverselectric power from the electrical power source 702 to the agitator pumpcontroller 406, the agitator motor controller 508, and/or the carbondioxide source valve controller 608.

FIG. 8 is a cut-away view of an ammonia delivery perforated tubing 800of the first system 100 that is coupled with an output port of the firstreturn pump RP01 and returns the aqueous solution 112 from the ammoniascrubber 122 and to the reaction chamber 124. The ammonia deliveryperforated tubing 800 is adapted and configured to return aqueoussolution 112 from the ammonia scrubber 122 and into the reaction chamber124, and may be or comprise perforated polyvinyl chloride piping and/orother suitable and substantively chemically inert material known in theart.

FIG. 9 is a cut-away view of a sulfur dioxide delivery perforated tubing900 of the first system 100 that circulates and returns the aqueoussolution 112 from the sulfur dioxide module 126 and to the reactionchamber 124. The sulfur dioxide delivery perforated tubing 900 isadapted and configured to return aqueous solution 112 from the sulfurdioxide module 126 and into the reaction chamber 124. The sulfur dioxidedelivery perforated tubing 900 may be or comprise perforated polyvinylchloride piping and/or other suitable and substantively chemically inertmaterial known in the art.

Referring now generally to the Figures and particularly to FIG. 10 andFIG. 11, FIG. 10 is a block diagram of a third alternate preferredembodiment of the present invention 1000 (hereinafter, “third system1000”) comprising the carbon dioxide module 202 coupled with the firstsystem 100. As disclosed in FIG. 11, the carbon dioxide module 202comprises a source of pressurized carbon dioxide 1100 and is adapted todeliver gaseous carbon dioxide into the water volume 104 and within thereaction chamber 124 via a length of the chemically inert tubing 144. Apressure release valve 1102 is coupled with the source of pressurizedcarbon dioxide 1100 and a carbon dioxide delivery tubing 1004 via thelength of the chemically inert tubing 144. The carbon dioxide perforateddelivery tubing 1004 located within the reaction chamber 124 and isadapted to accept carbon dioxide from source of pressurized carbondioxide 1100 and via the pressure release valve 1102. The carbon dioxidevalve controller 608 controls opening and closing of the pressurerelease valve 1102 and receives commands and electrical power from thecontrol module 200 via communications and power bus 132, whereby thecontrol system 118 directs, starts, stops and controls introduction ofcarbon dioxide into the aqueous solution 112 from the source ofpressurized carbon dioxide 1100. The carbon dioxide perforated tubing1004 may be or comprise perforated polyvinyl chloride piping or othersuitable and substantively chemically inert material known in the art.

FIG. 12 is an illustration of a motorized embodiment 1200 of the firstsystem 100. The motorized embodiment includes a motorized cab 1202 and awheeled trailer 1204, wherein the motorized cab 1202 is adapted todetachably engage with the wheeled trailer 1204 and transport portablean ammonia gas scrubber 1206, an RO/ED module 1208, a sulfur dioxidemodule 1210, a components holding tank 1212 and a resultant componentsholding tank 1212.

FIG. 13 is an illustration of a carbon dioxide generation 1300 modulethat accepts mammalian exhalation a source of gaseous carbon dioxide. Anenclosed animal barn 1300 substantively encloses a plurality ofmammalian livestock 1302-1306. An injection module 1308 receives carbondioxide sourced from the mammalian livestock 1302-1306 via a length ofthe tubing 144. The injection module 1308 pressurizes the receivedcarbon dioxide and injects the pressurized carbon dioxide into thepressurized carbon dioxide source 1100 via the tubing 144.

Referring now generally to the Figures and particularly to FIGS. 14, 15and 16, FIG. 14 discloses aspects and steps 14.00-14.22 of a sixthalternate preferred embodiment of the invented method (hereinafter, “thesixth method”), FIG. 15 discloses material, equipment and equipmentmodules 15A-15R that may be employed in one or more steps or aspects14.00-14.22 of the sixth method, and FIG. 16 discloses inventivematerials, aspects and elements 16A-16E that may optionally be appliedin an instantiation of the sixth method and various alternate preferredembodiments of the present invention.

More particularly FIG. 14 is a process diagram of the sixth method. Instep 14.00 a biomass 16A of organic residuals, e.g., chicken litterand/or other ammonia generating and/or comprising organic materials, ispositioned, preferably within an enclosure 102 as shown in FIG. 16, andenabled to emit a quantity of ammonium gas 15A into a mixture ofatmospheric gases 15B in step 14.02. The ammonium gas 15A may becaptured in step 14.02 as a component of a mixture of atmospheric gases15B or optionally selected from the atmospheric gases 15B. Optionalaspects and equipment related to the production of ammonium gas 15A areelaborated in FIG. 16.

The ammonium gas 15A and/or atmospheric gases 15B are optionally passedthrough an ammonium gas scrubber 15C in optional step 14.06. Theammonium gas 15A is delivered in step 14.08 into a reaction chamber 15D,and/or optionally as a component of the mixture of atmospheric gases 15Bof step 14.02 and/or as an output from the ammonium gas scrubber 15C.The ammonium gas 15A delivered into the reaction chamber 15D in step14.08 is thereupon brought into contact with, and permitted to reactwith, the second reactant sulfur dioxide 15A in step 14.09, whereupon anoutput mass of ammonium sulfate 15F is formed. The mass of ammoniumsulfate 15F is then transferred into a storage tank 15G in step 14.10and made available for immediate use, or alternately collected and madeavailable for later transport and use,

Referring now to steps 14.12 through 14.20, a second reactant sulfurdioxide 15E is disclosed to be generated from one or a combination ofsources. In optional step 14.12 a mass of elemental sulfur 15H issecured and thereupon is combusted in step 14.14 by means of a sulfurburning system 151. In one optional variation of the present invention,the sulfur burning system 151 is or comprises an a sulfur dioxide burnersystem as marketed by Harmon Systems International, LLC of Bakers field,Calif., whereby the second reactant sulfur dioxide 15E is generated bycombustion of the elemental sulfur 15H in optional step 14.16 by burningthe elemental sulfur 15H with a propane torch (not shown) to generate afirst mass of sulfur dioxide gas 15J containing the second reactantsulfur dioxide 15E.

Alternatively or additionally, a second mass of gaseous sulfur 15K maybe obtained and delivered in step 14.18. Further alternatively oradditionally, a third mass of gaseous sulfur 15L may be extracted from aliquid mass 15M of a solution containing sulfur in step 14.20 by anextraction system 15P.

The second reactant sulfur dioxide 15E as generated or obtained in steps14.14-14.20 may optionally be transferred into the scrubber in optionalstep 14.21.

The second reactant sulfur dioxide 15E as generated or obtained in steps14.14-14.20 is transferred into the reaction chamber 15D in step 14.22to enable reaction with the mass of ammonium gas 15A in step 14.10. Itis understood that the second reactant sulfur dioxide 15E may be orcomprise, in singularity or combination, the solid sulfur 15H of step14.12, the first mass of sulfur dioxide gas 15J of step 14.16, thesecond mass of gaseous sulfur 15K of step 14.18, and/or the third massof gaseous sulfur 15L of step 14.20.

Referring now to the Figures and particularly to FIG. 15, FIG. 15 is aschematic diagram of an additional optional embodiment of a productionfacility 15N wherein aspects of the sixth method, and other alternatepreferred embodiments of the invented method, may be instantiated orimplemented.

The source ammonium gas 15A is emitted from the organic source materialbiomass 16A containing ammonium and/or ammonium compounds. A first fan150.1 is adapted to withdraw the source ammonia gas 15A into an ammoniascrubber module 15C. The ammonia scrubber module 15C and the reactionchamber 15D are connected via a circulation system and are both coupledto the sulfur source enclosure 120. A sulfur dioxide generation module,either the sulfur gas 15A & 15J-15L from elemental sulfur combustion ofstep 14.14 of the method of FIG. 14 or extracted sulfur from sulfurwater source 15M, is also coupled with the reaction chamber 15D. As thereaction solution circulates through the scrubber 15C and reactionchamber 15D, the concentrate output is transferred into the storage tank15G.

It is understood that the ammonia scrubber 15C may be or comprise asuitable and commercially available gas scrubber known in the art, andthat the source fan may be comprised within the ammonia scrubber 15C. Itis further understood that the tubing connecting the source nitrogen gas15A and scrubber 15C may be or comprise polyvinyl chloride piping orother suitable and preferably substantively chemically inert materialknown in the art.

The concentrated output solution may thus include ammonium sulfate as asolute or component, whereby ammonium sulfate is produced in a mannerthat is in conformance one or more governmental, regulatory ororganizational standards and the resultant ammonium sulfate may receivea certification of a preferred or particular origin, such as a beingcertified, graded, trademarked or marked as a special type of organicsulfate. It is understood that the receipt of such certifications orauthorizations may increase the market value and perceived quality ofthe resultant ammonium sulfate of the concentrated output solution.

It is also understood that the system in FIG. 15 may includecommercially available equipment or their equivalents, wherein theammonia scrubber 15C may be or comprise, or be comprised within, a wetflue gas scrubber marketed by Deryck A Gibson Ltd. of Kingston Jamaica.In various alternate preferred embodiments of the present invention, thesource ammonia gas 15A is present as a mist, a spray or a waterfall asit circulates within the ammonia scrubber 15C. The reaction chamber 15Dmay comprise sheets, walls, a bottom wall and or/ceiling wall ofpolyvinyl chloride or other suitable material known in the art.

As indicated in FIGS. 14 and 15, the ambient air 15B and/or gases 15containing the collected NH3 and CO2 gasses are propelled by a first fan15O.1 to enter scrubber module 15C An optional second fan module 15O.2propels the ambient air 15B and/ or gases 15E, 15 j, 15K & 15L into thescrubber module 15C. An optional airway 15R enables propels the ambientair 15B and/ or gases 15E, 15 j, 15K & 15L into the scrubber module 15Cby an alternate route. An optional third fan module 15O.3 propels theambient air 15B and/ or gases 15E, 15 j, 15K & 15L directly into thereaction chamber 15D.

FIG. 16 demonstrates a yet additional preferred embodiment of thecomposting apparatus, wherein ammonia gas 15A is produced by highlyselective aerobic bacteria 16D action with the biomass 16A and withoutadding external heat. The composting building, which may be a barn, ashed, a greenhouse, or a specially constructed dedicated facility, canalso serve as the ammonia source chamber that contains and shields theorganic residuals biomass 16A. According to an embodiment of theinvention, the floor of the facility is contained of a layer of organicresiduals biomass 16A, as the source of ammonia gas 15A, and is shieldedto prevent noxious gases from escaping. A composting trench is built atthe same positions as label 16.02 to insulate the biomass from heatloss, and to allow easy aeration and physical movement of the biomass.The composting trench also contains a forced aeration system 16C,injecting oxygen gases to facilitate the action of a mass of aerobicbacteria 16D.

Aerobic bacteria 16D are provided to highly selectively convert all orsubstantially all of the waste amino acids, proteins, uric acid and anyother available nitrogen com pounds in the biomass into NH3 and/or NH4and CO2. Preferably, the specific strains of aerobic bacteria 16D usedin the present invention include uricolytic bacteria such as Bacilluspasteurii and/or Peptostreptococcus anaerobius, Clostridium sticklandii,Clostridium aminophilum, and Eubacterium pyruvativorans. Thermophilicbacteria are preferred because their presence reduces the population ofharmful bacteria such as E.coli, Salmonella and fecal coliform bacteria.

As the composting process commences, a rototiller 16B may be used tomix/agitate and aerate the biomass. In a preferred embodiment, a hoodmay be used to capture rising water vapor and/or NH3 and/or NH4 andCO2from the biomass 16A as it generates heat. An intake channel 16Edelivers water vapor and/or NH3 and/or NH4 15A from the enclosure 120and into the scrubber 15C.

Referring now generally to the Figures and particularly to FIGS. 17, 18and 19, FIG. 19 discloses aspects of a seventh alternate preferredembodiment of the invented method (hereinafter, “the seventh method”),FIGS. 17 and 18 disclose material, equipment and equipment modules1700-1732 that may be employed in one or more steps or aspects of theseventh method, and FIG. 19 discloses inventive materials, aspects andelements 1900-1914 that may optionally be applied in an instantiation ofthe seventh method and various alternate preferred embodiments of thepresent invention.

Referring to FIGS. 17 through 19, a preferred embodiment of a compostingapparatus 1700 and a method of producing solid and/or concentratedorganic ammonium sulfate product by highly selective aerobic bacteria16D action without adding external heat, are shown and described.Composting apparatus 1700 is preferably located inside of a compostingbuilding 1704. Composting building 1704 may be a barn, a shed, or agreenhouse. In other embodiments, composting building 1704 may simply bea cover or box covering composting trench 1702. Composting building 1704includes an input end 111, an output end 1713, and a composting trench1702. Preferably, composting trench 1702 is the receptacle used forcomposting. Preferably, composting building 1704 contains and shieldsthe composting trench 1702 so that noxious gases cannot escape into theenvironment. Composting trench 1702 preferably contains the heatgenerated by the aerobic bacteria 16D action, insulates the biomass fromheat loss, and allows easy aeration and physical movement of thebiomass. Composting building 1704 preferably contains the means tocontrol the temperature, the moisture, the pH, and the nitrogen contentof the biomass in composting apparatus 1700. Composting building 1704preferably includes steep eaves or a narrowed roof area to allow a moreefficient capture and removal of gasses and water vapors from inside theatmosphere of composting building 1704. Composting building 1704 mayalso include a louvered opening 1732 at the input end 1711. Preferably,louvered opening 1732 may be used for air control. In other embodiments,louvered opening 1732 may be omitted or replaced with another suitablemechanism.

In a preferred embodiment, composting trench 1702 is from about 1 footto about 10 feet deep; more preferably from about 2 feet to about 6 feetdeep; and most preferably from about 4 feet to 5 feet deep. In apreferred embodiment, composting trench 1702 is from about 50 feet toabout 500 feet long; more preferably from about 100 feet to about 350feet long; and most preferably from about 200 to about 300 feet long. Ina preferred embodiment, composting trench 1702 is from about 3 feet toabout 25 feet wide; more preferably from about 5 feet to about 20 feetwide; and most preferably from about 8 feet to about 14 feet wide. In apreferred embodiment, the dimensions of composting trench 1702 are asfollows: about 4 feet deep, about 250 feet long, and about 10 to about12 feet wide. In other embodiments, composting trench 1702 may havedimensions greater than, less than, or different from those describedabove.

In a preferred embodiment, composting trench 1702 is configured to holdfrom about 20 days to about 50 days of manure, and more preferably fromabout 25 days to about 30 days of manure. In other embodiments,composting trench 1702 is configured to hold less than about 20 days ofmanure or greater than about 50 days worth of manure. In a preferredembodiment, composting trench 1702 is configured such that the last fewdays of compost, preferably the last three days of compost, are covered.The cover captures gases that will be used for bioburden reductionand/or for killing the bacteria 16D as the composting process ceases.

Referring to FIG. 2, composting trench 1702 includes airflow ducts 1706and a heat conducting water system 1712. Preferably, each of the airflowducts 1706 and heat conducting water system 1712 is comprised of aplurality of pipes that are perpendicular to a longitudinal axis ofcomposting trench 1702 (i.e., are perpendicular to flow of the compost).The pipes in the airflow ducts 1706 are preferably separate from thepipes in heat conducting water system 1712. Preferably, each of thepipes in the airflow ducts 1706 and each of the pipes in heat conductingwater system 1712 is about 12 feet long and situated every few feet,i.e., about every 5 feet. Preferably, airflow ducts 1706 are used toregulate, provide, and/or supply airflow to various sections ofcomposting trench 1702. Preferably, heat conducting water system 1712 isused to distribute the heat generated by the aerobic composting processto various sections of composting trench 1702. A plurality of manifoldsand/or valves within these pipes may be used to distribute the gas/heatto the compost. Preferably, the pipes may be perforated to allow fortransport of the process gases throughout composting trench 1702. Forexample, the pipes may transport gases such as air, oxygen and/orammonia produced from the composting process of the present invention tovarious sections of composting trench 1702. In this manner, the gasesmay be distributed where needed. Additionally, composting trench 1702may include vents. In other embodiments, airflow ducts 106 and/or heatconducting water system 1712 may be omitted and/or replaced with anothersuitable mechanism. In yet other embodiments, the pipes may be situatedparallel to the longitudinal axis of composting trench 1702. In yetother embodiments, the pipes may not be perforated. In yet otherembodiments, the pipes for airflow ducts 1706 and the pipes for heatconducting water system 1712 may not be separate. In yet otherembodiments, heat may be controlled and/or distributed via electricalmeans and/or other non water-based means. In other embodiments, othermeans of distributing heat and/or controlling may be used, in lieu of,or in addition to, the means of distributing and/or controlling heatdescribed above.

Referring to FIG. 18, composting trench 1702 of composting apparatus1700 includes crawl space 1708 at top of composting trench 1702.Preferably, crawl space 1708 is used to enable access to the pipes forthe purpose of reconfiguring the pipes and/or for maintenance of thepipes. In other embodiments, crawl space 1708 may be omitted or replacedby another suitable mechanism.

In a preferred embodiment, the temperature of the biomass does notexceed about 70 degree C. during the aerobic composting processaccording to present invention. Most preferably, the temperature of thebiomass is kept between 50 degree C. and 70 degree C. In order toregulate the compost temperature, the heat generated by the aerobiccomposting process may be distributed as follows. For example, theaerobic composting process heats water in the pipes of heat conductingwater system 1712. These pipes may distribute heat up and downcomposting trench 1702 by distributing hot water up and down compostingtrench 1702. For example, hot water may be sent to any part ofcomposting trench 1702 via these pipes from a high temperature sectionof composting trench 1702.

In a preferred embodiment, a hood may be used to capture rising watervapor and/or NH₃ and/or NH₄ and CO₂ from the biomass as it generatesheat. In yet other embodiments, in lieu of, or in addition to, using ahood to capture rising water vapor or NH₃ and/or NH₄ and CO₂ at least aportion of the roof of composting building 1704 may also be used.Preferably, the roof of the composting building 1704 includes steepeaves or a narrowed roof area to allow a more efficient capture andremoval of NH₃ and/or NH₄ and CO₂ from inside composting building 1704.

The present invention generally operates as follows. Manure is collectedfrom a CAFOs facility on a continuing basis, as soon as feasible.Preferably, manure is collected from a CAFOs facility within 12 hours ofproduction. The collected manure has a moisture content of about 70-80%by weight. A source of carbon is added, preferably at a ratio of manureto carbon source of about 3:2, resulting in a biomass with a moisturecontent of preferably about 30%-70% by weight. Most preferably, theresulting biomass has a moisture content of about 50% by weight.Preferably, the source of carbon is sawdust. Other sources of carbon maybe used in lieu of, or in conjunction with, sawdust. In addition toproviding a carbon source during the aerobic composting process, thenature of the carbon source may also provide porosity to the biomass,improving the speed and efficiency of the capture of composting gases.

According to an embodiment of the invention, the floor of a CAFOsfacility containing manure may be washed periodically, and the water andmanure may be collected in a containment pool. The containment pool ispreferably enclosed or shielded, such that the NH₃ and CO₂ gasses fromthe manure composting process cannot escape into the environment. Theshielding or enclosure of the containment pool preferably contains asuitable air handling system manufactured to withstand the corrosionassociated with NH₃ and CO₂ gases, which is used to collect the NH₃ andCO₂ gasses and to transfer the collected NH₃ and CO₂ gasses to one ormore collection tank(s) 1801 which contain an aqueous solution.According to an embodiment of the invention, additional CO₂ gasses maybe collected from the atmosphere of the CAFOs facility by means of asuitable air handling system manufactured to withstand the corrosionassociated with NH₃ and CO₂ gases. The CO₂ gases collected from theatmosphere of the CAFOs facility are transferred via the air handlingsystem to one or more collection tank(s) 1801.

In a preferred embodiment, the source of carbon includes carbon tonitrogen in the ratio of at least about 6:1. In other embodiments, thevolume/amount of manure and/or carbon source used in the input may vary,depending on, for example, the capacity of composting trench 1702. Inyet other embodiments, the carbon to nitrogen ratio of the source ofcarbon may be less than about 6:1 or greater than about 6:1. In yetother embodiments, an additional source of carbon may not be added tothe manure, and the manure alone may be used in the composting processof the present invention.

Referring to FIG. 17, the input 1710 of the present invention ispreferably manure mixed with a source of carbon to form a biomass havinga high solids content for aerobic composting. The resulting biomass isspread around composting trench 1702, and is moved through compostingtrench 1702 as the composting process progresses. Preferably, the amountof biomass used in input 1710 is a day's worth of manure. This amount,of course, will vary depending upon, for example, the amount ofavailable manure and/or sawdust and/or the size of composting apparatus1700. A day's worth of biomass is loaded onto composting trench 1702daily. As such, a new input may be created everyday and identified as“day 1 compost,” “day 2 compost,” “day 3 compost,” etc. For example, thefirst day's biomass would be labeled as “day 1 compost.” The next day,at about the same time, the previous day's biomass would be moved downthe length of the composting trench 1702, making room for the secondday's biomass. Second day's biomass is loaded onto composting trench 102and labeled as “day 2 compost,” and so forth. Preferably, the biomass isadded at a specified time of day. To make room for the next day'sbiomass, the previous day's biomass is moved down composting trench 1702using a rototiller (available from, for example Farmer Automatic ofAmerica). This leaves an open space for the next day's biomass incomposting trench 1702. Preferably, each day's biomass is moved about 5feet to about 10 feet down composting trench 1702.

Temperature, pH and moisture content of the biomass are controlled byaeration of the biomass both by a physical moving and mixing process,and by the addition of O₂ into composting trench 1702. Within thebiomass, the dissolved ammonia gas NH₃ is in a chemical equilibrium withthe NH₄. The ratio of NH₄ to NH₃ in this equilibrium is pH dependent.Preferably, the pH of the biomass is controlled to keep the alkalinitylevel of the biomass high so that most of the NH₄ in the biomass isconverted to NH₃ and released into the air, and not nitrified by thebacteria 16D present in the biomass. Preferably, the pH of the biomassis also controlled so that the aerobic bacteria 16D are not killed bythe NH₃ production. In a preferred embodiment, the pH of the biomass isbetween 8.0 and 10.1.

Each day's biomass may be moved once during the day, several timesduring the day, and/or continuously throughout the day. As thecomposting process commences, a rototiller may be used to mix/agitateand aerate the biomass. In other embodiments, other means of movingand/or aerating the biomass may be used in lieu, or in conjunction with,the rototiller. In yet other embodiments, biomass may not be added tothe composting trench 1702 daily, but may be added more often than that,or less often than that, i.e., every other day. In this manner, the nextload of biomass may be added the same day as the previous load, or everyother day. The amount of biomass and time intervals between eachaddition may vary.

In a preferred embodiment, O₂ is added to the biomass during the aerobiccomposting process to facilitate the composting reaction. Preferably,the form of O₂ addition is air. Preferably, the rate of O₂ addition isdetermined by the temperature of the biomass 16A. Preferably, O₂ isadded to any one or more of the day 1 to day 15 allotments of biomass.Preferably, the amount of O₂ added over the length of composting trench1702 decreases. In this manner, preferably, the amount of O₂ added onday 10 is less than the amount of O₂ added on day 1. In otherembodiments, other sources of O₂ may be used and/or other means ofcontrolling O₂ addition may be used. Air ducts 1706 may be used toregulate airflow. This may ensure that bacteria 16D in the biomassreceive an adequate supply of O₂ to complete the composting process. Inother embodiments, other means of regulating airflow, in lieu of, or inconjunction with air ducts 1706, may be used.

Aerobic bacteria 16D are provided to highly selectively convert all orsubstantially all of the waste amino acids, proteins, uric acid and anyother available nitrogen compounds in the biomass into NH₃ and/or NH₄and CO₂. Preferably, the specific strains of aerobic bacteria 16D usedin the present invention include uricolytic bacteria such as Bacilluspasteurii and/or Peptostreptococcus anaerobius, Clostridium sticklandii,Clostridium aminophilum, and Eubacterium pyruvativorans. Thermophilicbacteria are preferred because their presence reduces the population ofharmful bacteria such as E. coli, Salmonella and fecal coli-formbacteria. During the aerobic composting process, the biomass shouldremain at a temperature of 50 C. to 70 C. to promote the growth ofthermophilic bacteria. The heat to maintain this temperature is suppliedby the aerobic composting process and is distributed by heat conductingwater system 1712. Regular aeration of the biomass helps to regulate thetemperature as well as supplies the oxygen to the bacteria 16D. It isnot necessary to add external heat to the aerobic composting process tomanufacture ammonium sulfate according to the present invention.

As the aerobic process progresses, the aerobic bacteria 16D highlyselectively convert all or substantially all of the waste amino acids,proteins, uric acid and any other available nitrogen compounds in thebiomass into NH₃ and/or NH₄ and CO₂. The resulting NH₃ and CO₂ gassesare collected from the atmosphere of the composting building 1700 bymeans of hood 1714 and/or air flow ducts 1706, or another suitable airhandling system manufactured to withstand the corrosion associated withNH₃ and CO₂ gases. Preferably, the air handling system should be capableof changing the building volume of air in less than one hour.

Referring to FIG. 19, the air containing the collected NH₃ and CO₂gasses is delivered to one or more collection tank(s) 1901 which containan aqueous solution. The air containing the collected NH₃ and CO₂ gassesis forced by the air handling system to enter the collection tank(s)1901 through an array of diffuser units 1902. Preferably, the diffuserunits 1902 are adapted to release the collected NH₃ and CO₂ gases intothe collection tank(s) 1901 as small gas bubbles, preferably 5 micronsto 10,000 microns in diameter. Preferably, the number and size of thediffuser units 1902 is sufficient to ensure that substantially all ofthe collected NH₃ and CO₂ gasses are removed from the air as the airpasses through the collection tank(s) 1901. After the passage throughthe collection tank(s) 1901, the air handling system may recycle the airback to the atmosphere of the composting building 1700 so that anyunabsorbed NH₃ and CO₂ remaining in the air may be added back intocomposting trench 1702, and/or may be collected for future use orcommercial purposes. The captured NH₃ and/or NH₄ react with the aqueoussolution in collection tank(s) 1901, and are converted to ammoniumhydroxide. The ammonium hydroxide reacts with captured CO₂ to formammonium polycarbonate. Preferably, the process is allowed continueduntil the pH in the collection tank(s) 1901 reaches 8.5 to 9.35.Preferably, the process is allowed to continue until the concentrationof ammonium polycarbonate in the aqueous solution of the collectiontank(s) 1901 reaches a concentration of between 1,600 ppm and 4,500 ppmas measured with an electrical conductivity meter.

In the preferred embodiment, after the concentration of ammoniumpolycarbonate in the aqueous solution of the collection tank(s) 1901reaches a concentration of between 1,600 ppm and 4,500 ppm, the aqueoussolution containing ammonium polycarbonate, ammonium hydroxide and CO₂,is removed from the collection tank(s) 1901 through a first pipingsystem 1903, and is transferred to one or more pre-osmosis holdingtank(s) 1904. In order to increase the concentration of the ammoniumpolycarbonate in the aqueous solution, the aqueous solution containingammonium polycarbonate, ammonium hydroxide and CO₂ is transferred frompre-osmosis holding tank(s) 1904 to one or more reverse osmosis devices206 through a second piping system 1905. The reverse osmosis devices mayinclude a DOW (TM) FILMTEC (TM) XLE-440 reverse osmosis membrane, or asimilar reverse osmosis membrane. The reverse osmosis process allowswater to be removed from the aqueous solution resulting in a moreconcentrated ammonium polycarbonate solution. The removed water istransferred from reverse osmosis device(s) 1906 through a third pipingsystem 1907 to a water holding tank 1908, and may be reused in theprocess or discarded. The reverse osmosis process may be repeated asnecessary to increase the concentration of the ammonium polycarbonate inthe aqueous solution. In other embodiments, the reverse osmosis processmay be replaced by other processes suitable for increasing theconcentration of the ammonium polycarbonate solution in the aqueoussolution, or it may be omitted.

The aqueous solution containing concentrated ammonium polycarbonate istransferred from reverse osmosis device(s) 1906 through a fourth pipingsystem 1909 to one or more reaction tank(s) 1910. Sulfate 1912 is addedto reaction tank(s) 1910 at a ratio of approximately 5 pounds of sulfatefor each 1 gallon of ammonia solution. In certain alternate preferredembodiments of the seventh method, the source of sulfate 1912 preferablycomprises Organic Materials Review Institute (“OMRI”) certified organicgypsum. According an embodiment of the present invention, in order toimprove the yield of ammonium sulfate, excess sulfate 1912 may be addedto reaction tank(s) 1910, at a ratio of approximately 6 pounds ofsulfate for each 1 gallon of ammonia solution.

The temperature of the aqueous solution containing concentrated ammoniumpolycarbonate and sulfate 1912 in reaction tank(s) 1910 is raised to50.degree. C. or allowed to rise to 50.degree. C. due to the chemicalreaction between the ammonium carbonate and sulfate 1912. During theinitial reaction period (preferably four hours), the aqueous solutioncontaining concentrated ammonium polycarbonate and sulfate 1912 is mixedand circulated inside reaction tank(s) 1910, resulting in the formationof ammonium sulfate suspension 1915 and calcium carbonate. The pressuremay be allowed to increase in the reaction tank(s) 1910 in order toincrease the rate and yield of ammonium sulfate. Preferably, thepressure is allowed to increase to two atmospheric pressures or greater.Calcium carbonate is allowed to settle to the bottom of reaction tank(s)1910 in the form of the calcium carbonate sludge. In a preferredembodiment, the calcium carbonate sludge is removed from reactiontank(s) 1910 through a floor drain and a fifth piping system 1916 to oneor more bag filters 1917 which capture the calcium carbonate sludge. Theresulting captured calcium carbonate sludge can be recovered and used asa separate product for various agricultural and non-agriculturalpurposes.

After the initial reaction period (preferably four hours), the aqueoussolution containing concentrated ammonium polycarbonate, sulfate 1912and ammonium sulfate suspension 1915 is moved from reaction tank(s) 1910through a sixth piping system 1913 to one or more holding area tank(s)1914, where the presence of unreacted sulfate 1912 in said aqueoussolution allows the formation of ammonium sulfate suspension 1915 toproceed for an additional period of time, preferably for more than 5days. Most preferably, the formation of additional ammonium sulfatesuspension 1915 in holding area tank(s) 1914 is allowed to proceed for aperiod of 10 days.

According to an embodiment of the invention, the resulting ammoniumsulfate suspension 1915 may be centrifuged to remove excess water inorder to concentrate the ammonium sulfate suspension 1915 to a desireddensity for use as a liquid fertilizer. In other embodiments, thecentrifugation process may be replaced by other processes suitable forincreasing the concentration of the ammonium sulfate suspension 1915.According to an embodiment of the invention, the ammonium sulfatesuspension 1915 may be dried to form crystals of dry ammonium sulfate.The resulting liquid or dry ammonium sulfate is certifiable as organic.The term “organic” as used herein, is a labeling certification term thatrefers to an agriculture product produced in accordance with the Code ofFederal Regulations (“CFR”) Title 7 (Subtitle B, Chapter I, SubchapterM, Part 205).

The foregoing disclosures and statements are illustrative only of thePresent Invention, and are not intended to limit or define the scope ofthe Present Invention. The above description is intended to beillustrative, and not restrictive. Although the examples given includemany specificities, they are intended as illustrative of only certainpossible configurations or aspects of the Present Invention. Theexamples given should only be interpreted as illustrations of some ofthe preferred configurations or aspects of the Present Invention, andthe full scope of the Present Invention should be determined by theappended claims and their legal equivalents. Those skilled in the artwill appreciate that various adaptations and modifications of thejust-described preferred embodiments can be configured without departingfrom the scope and spirit of the Present Invention. Therefore, it is tobe understood that the Present Invention may be practiced other than asspecifically described herein. The scope of the present invention asdisclosed and claimed should, therefore, be determined with reference tothe knowledge of one skilled in the art and in light of the disclosurespresented above.

We claim:
 1. A method comprising: a. forming a volume of fluid water; b.burning sulfur in the presence of oxygen to form sulfur dioxide; c.exposing the volume of fluid water to the sulfur dioxide, whereby thevolume of fluid water is transformed into an aqueous solution having apH below 5; d. exposing the aqueous solution to an atmospheric gasvolume comprising gaseous ammonia; and e. removing a component of theaqueous solution from the aqueous solution, the component comprisingnitrogen compounds.
 2. The method of claim 1, wherein the componentcomprises ammonium sulfate.
 3. The method of claim 1, wherein thecomponent is removed from the aqueous solution in a solution comprisinga portion of the aqueous solution.
 4. The method of claim 1, furthercomprising: f. continuing to expose the aqueous solution to the sulfurdioxide until a pH measurement of the aqueous solution of approximatelyfour is generated; and g. halting the exposure of the sulfur dioxideuntil a pH measurement of the aqueous solution of approximately five isgenerated; and h. resuming exposure of the aqueous solution to thesulfur dioxide until a pH measurement of the aqueous solution ofapproximately four is again generated.
 5. The method of claim 1, furthercomprising enclosing a source volume of atmosphere at approximatelystandard atmospheric pressure, the source volume of atmosphereadditionally comprising gaseous ammonia from which the gaseous ammoniaintroduced into the aqueous solution is sourced.
 6. The method of claim1, wherein the volume of gaseous ammonia includes molecules of NH3 andmolecules of NH4+.
 7. The method of claim 1, wherein the volume gaseousammonia is at least partially generated from mammalian dung or avianfeces.
 8. The method of claim 1, wherein the gaseous sulfur dioxide ispressure injected into the volume of fluid water to form the aqueous. 9.A method comprising: a. collecting an organic waste mass containingammonium, the waste mass comprising bacteria, wherein the bacteriagenerate a volume of gaseous ammonia; b. forming a volume of fluidwater; c. burning sulfur in the presence of oxygen to form sulfurdioxide; d. exposing the volume of fluid water to the sulfur dioxide,whereby the volume of fluid water is transformed into an aqueoussolution having a pH below 5; e. exposing the aqueous solution to thegaseous ammonia; and f. removing a resultant component comprising anitrogen compound from the aqueous solution.
 10. The method of claim 9,wherein the resultant component comprises ammonium sulfate.
 11. Themethod of claim 9, wherein the resultant component is at least partiallyremoved from the aqueous solution in combination with a portion of theaqueous solution.
 12. The method of claim 9, further comprising aeratingthe waste mass by mechanical disturbance, whereby a rate of generationof gaseous ammonia by the bacteria is increased.
 13. The method of claim12, wherein the aeration of the organic waste comprises mechanicaldisturbance.
 14. The method of claim 9, further comprising enclosing thewaste mass, whereby the gaseous ammonia is collected prior tointroduction of the gaseous ammonia into the fluid water.
 15. The methodof claim 11, further comprising substantively removing the componentfrom the volume fluid water while simultaneously introducing additionalgaseous ammonia and additional gaseous sulfur dioxide into the volume offluid water
 16. A system comprising: a. a volume of fluid water; b. asulfur burner module, the sulfur burner module adapted to form sulfurdioxide by a sustained ignition of sulfur. c. means to inject the sulfurdioxide into the volume of fluid water, whereby the sulfur dioxide andthe volume of fluid water form an acidic aqueous solution; d. means toexpose a gaseous volume comprising ammonia to the acidic aqueoussolution, whereby the acidic aqueous solution absorbs ammonia; and e.means to remove a resultant component from the aqueous solution.
 17. Thesystem of claim 16, further comprising an enclosure, the enclosureadapted to substantively contain the gaseous volume.
 18. The system ofclaim 16, wherein the means to remove the resultant component from theaqueous solution comprises a reverse osmosis apparatus.
 19. The systemof claim 16, wherein the means to remove the resultant component fromthe aqueous solution comprises an electro-dialysis apparatus.
 20. Thesystem of claim 16, wherein resultant component comprises ammoniumsulfate.